EP2239027B1 - Method and device for producing vacuum in a petroleum distillation column - Google Patents

Method and device for producing vacuum in a petroleum distillation column Download PDF

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Publication number
EP2239027B1
EP2239027B1 EP08865376.1A EP08865376A EP2239027B1 EP 2239027 B1 EP2239027 B1 EP 2239027B1 EP 08865376 A EP08865376 A EP 08865376A EP 2239027 B1 EP2239027 B1 EP 2239027B1
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Prior art keywords
gas
vacuum
steam
outlet
vapour
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EP08865376.1A
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German (de)
English (en)
French (fr)
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EP2239027A1 (en
EP2239027A4 (en
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Valery Grigorievich Tsegelsky
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/10—Vacuum distillation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/10—Vacuum distillation
    • B01D3/105—Vacuum distillation with the use of an ejector for creating the vacuum, the ejector being placed between evaporator or distillation devices
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G7/00—Distillation of hydrocarbon oils
    • C10G7/06—Vacuum distillation

Definitions

  • the invention relates to methods and plants for producing vacuum in a vacuum oilstock distillation column by supplying steam to the vacuum column and/or to the oilstock, an can be used in the oil processing industry to produce vacuum in a vacuum rectification column for distilling black oil.
  • a method for producing vacuum in a vacuum oilstock distillation column black oil
  • a vapour ejector consisting of a series of gas-gas ejectors fed with steam used as a high pressure gas supplied from an external source
  • vapour-gas mixture from a gas-gas ejector to a condenser followed by cooling thereof and condensing vapour phase of the vapour-gas mixture is also known from said patent.
  • the above indicated patent also teaches a plant for producing vacuum in a vacuum oilstock distillation column comprising a gaseous vapour discharge pipeline, a gas-gas ejector and a condenser; in the plant the gas-gas ejector at a low-pressure gas inlet end is connected to the gaseous vapour discharge pipeline, at a high-pressure gas inlet it is connected to the external vapour source, at a gaseous vapour outlet it is connected to a condenser inlet having a gaseous mixture and a condensate outlet.
  • a drawback of the known method and the plant consists in using external steam source and discharging water condensate in a mixture with petroleum fraction from the plant that leads to environmental pollution and a loss of a distillation product.
  • Another drawback is a considerable energy consumption caused by using great amounts of steam and water required to perform a multistage compression of the vapour-gas medium using gas-gas ejectors and a condensation of the steam between the stages.
  • a method for fractioning of two distillable mixtures in a vacuum column comprising feeding of water and a mixture of a first and a second distillable hydrocarbonaceous compounds into the vacuum column and removing a first product stream comprising the first distillable hydrocarbonaceous compound from bottom of the vacuum column; withdrawing water vapour and the second distillable hydrocarbonaceous compound vapour from overhead of the vacuum column; admixing the overhead vapour stream with a liquid recycle stream and passing the resultant mixture stream into a first condenser; supplying condensate formed in the first condenser and non-condensable vapour into an overhead receiver; separation in the overhead receiver the condensate into the second distillable hydrocarbonaceous compound withdrawn as the second product stream and aqueous liquid stream comprising at least 60 mole percent water; supplying the aqueous liquid stream from the overhead receiver into a steam generator wherein by indirect heat exchange against a high temperature heating agent the aqueous liquid stream is vaporized to form moderate pressure steam; producing vacuum in the overhead receiver
  • Gas-vapour medium which is evacuated from vacuum column overhead during black oil distillation process comprises non-condensable gases, water vapour and condensable hydrocarbons of wide composition range. Part of these condensable hydrocarbons (light hydrocarbons) can be condensed only at pressure higher than vacuum column overhead pressure at given temperature of cooling agent supplied into the first condenser. Therefore light hydrocarbons vapour can not be removed from the vacuumized overhead receiver.
  • this light hydrocarbons vapour is compressed in the steam-jet ejector and condensed together with steam in the second condenser; after that mixture of the light hydrocarbons condensate and water condensate is supplied from the seal drum into the overhead gas-vapour stream. Since the overhead gas-vapour stream is under vacuum, this light hydrocarbons condensate will be evaporated and will be supplied via the overhead receiver to the steam-jet ejector again. Since this light hydrocarbons condensate is not removed from the described technological process of fractioning, it will lead to vacuum losses and termination of fractioning process.
  • the drawback of the above method is that the same steam generator produces both steam which serves as motive stream for the steam-jet ejector and steam which serves as heating agent and carries heat from the steam generator to the vacuum column to provide processes of heat and mass transfer in the column. It does not make possible to reduce energy consumption for vacuum production since distillate which leaves the vacuum column can not be used as heating agent for generation of steam fed to the steam-jet ejector. Within the framework of the above method distillate temperature can not be higher than temperature of steam leaving the steam generator.
  • heating agent stream at high temperature is supplied from an external source to the steam generator for producing moderate pressure steam, this requires considerable energy consumption for production of vacuum in the column.
  • the closest prior art in part of a method as a subject matter of the invention in terms of technical entity and attained result is represented by a method for producing vacuum in a vacuum petroleum distillation column that comprises pumping out a vapour-gas medium from the vacuum column with a gas-gas ejector fed with a high-pressure gas to form at an outlet of the gas-gas ejector a vapour-gas mixture having a pressure greater than a pressure of the vapour-gas medium, feeding the vapour-gas mixture and pumping a liquid to a liquid-gas jet device, mixing the vapour-gas mixture and the liquid in the liquid-gas jet device to form a gas-liquid mixture at an outlet thereof, supplying the gas-liquid mixture from the liquid-gas jet device to a separator to separate the mixture into a compressed gas and a liquid, evacuating the compressed gas from the separator for the intended use thereof and supplying the liquid to the inlet end of the pump ( see, patent RU 2310678 , IPC B01D 3/10, 20.11.2007).
  • a plant for producing vacuum in a vacuum petroleum distillation column that comprises a pipeline for discharging vapour-gas medium from the vacuum column, a gas-gas ejector, a condenser, a liquid-gas jet device, a separator, a pump and an additional pump; in the plant the gas-gas ejector at a low-pressure gas inlet is connected to the pipeline for discharging vapour-gas medium from the vacuum column, the liquid-gas jet device at a liquid inlet is connected to the pump outlet end, at a gas-liquid outlet it is connected to the separator having a compressed gas outlet and a liquid outlet connected to the pump inlet ( see, patent RU 2310678 , IPC B01D 3/10, 20/11/2007).
  • the main drawback of the above method for producing vacuum in a vacuum oilstock (inter alia black oil) distillation column and the plant for implementing thereof is a high power a pump of a vacuum producing device consumes especially in a case the oilstock distillation is performed with feeding steam to the vacuum column operating at a pressure lower than 6 kPa.
  • a problem the present invention is intended to solve is a production of a high-pressure gas fed to a gas-gas ejector from a water-containing medium formed while the plant is operating using heat of oil distillates or oilstock as well as reducing environmental pollution due to the bleeding the water-containing medium comprising hydrocarbons by organizing its circulation within a closed contour in the plant.
  • a technical result consists in that the energy consumed to produce vacuum is reduced, vacuum depth is increased, environmental pollution is reduced, and no steam supplied from an external source is now required.
  • a method for producing vacuum in a vacuum oilstock distillation column comprises pumping out a vapour-gas medium from the vacuum column using a gas-gas ejector fed with a high-pressure gas to form at an outlet of the gas-gas ejector a vapour-gas mixture having a pressure greater than a pressure of the vapour-gas medium at an inlet thereof, supplying the vapour-gas mixture to a condenser followed by cooling thereof and forming a gas mixture and a vapour phase condensate, supplying the gas mixture and pumping a liquid to a liquid-gas jet device with a pump, mixing the gas mixture and the liquid in the liquid-gas jet device to form a gas-liquid mixture at an outlet thereof, supplying the gas-liquid mixture from the liquid-gas jet device to a separator to separate the mixture into a compressed gas and a liquid, discharging the compressed gas for the intended use thereof
  • the steam having a pressure in the range of 0.2 - 0.6 MPa is preferably produced in the steam generator.
  • a portion of the water-containing condensate which is not evaporated in the steam generator is preferably evacuated to the additional separator, at the same time this portion of the water-containing condensate is preferably cooled in a heat exchanger prior to evacuation to the additional separator.
  • the steam from the steam generator can be fed to the vacuum oilstock distillation column via an additional gas-gas ejector, thus the latter can additionally evacuate the vapour-gas medium from said vacuum column.
  • a plant for producing vacuum in a vacuum oilstock distillation column comprising a pipeline for evacuating a vapour-gas medium from the vacuum oilstock distillation column, a gas-gas ejector, a condenser, a liquid-gas jet device, a separator, a pump and an additional pump, wherein the gas-gas ejector is connected at a low-pressure inlet thereof to the pipeline for evacuating a vapour-gas medium from the vacuum column and at a vapour-gas mixture outlet thereof is connected to the condenser inlet, the latter has a condensate outlet and a gas mixture outlet connected to the liquid-gas jet device via a gas inlet, wherein the liquid-gas jet device is connected to the pump outlet via a liquid inlet and to the separator via a gas-liquid outlet, the separator has a compressed gas outlet and liquid outlet connected to the pump inlet, the
  • the steam generator can have a non-evaporated condensate outlet connected to the additional separator, at the same time the non-evaporated condensate outlet of the steam generator can be connected to the additional separator inlet via a heat exchanger.
  • the steam outlet of the steam generator can be additionally connected to the vacuum oilstock distillation column and/or to the pipeline for supplying oilstock to this vacuum column.
  • the steam outlet of the steam generator can be connected to the high-pressure gas inlet of the gas-gas ejector and/or to the vacuum oilstock distillation column via heat exchange pipes for heating steam in a furnace.
  • An additional gas-gas ejector connected at a low-pressure gas inlet thereof to the pipeline for evacuating vapour-gas medium from said vacuum column and connected at the steam inlet to the steam outlet of the steam generator can be mounted on a pipeline supplying the steam to the vacuum column.
  • the condenser can consist of a vapour condensing device and a phase separator, in this case an inlet of the vapour condensing device is connected to the vapour-gas mixture outlet of the gas-gas ejector, a biphasic mixture outlet of the vapour condensing device is connected to an inlet of the phase separator having a condensate outlet and a gas mixture outlet.
  • Disclosed method and plant for accomplishing thereof allow vacuum to be produced in a vacuum oilstock distillation column by a two-stage compression of a vapour-gas medium with an intermediate condensation of the vapour phase between the stages.
  • a main part of working fluid of the high-pressure flow (an ejecting stream) fed both to the gas-gas ejector (steam from the water-containing condensate) and to the liquid-gas jet device (a working fluid) circulates within a closed contour.
  • Relatively small substitution of the circulating working fluid occurs due to the formation of a condensate of the vapour phase of the vapour-gas medium pumped out from the vacuum oilstock distillation column.
  • a small substitution of the circulating working fluid with the substance from an external source is also possible, especially at the second stage of compression.
  • a hydrocarbon-containing liquid as a working fluid pumped to the liquid-gas jet device.
  • Diesel and gas oil fractions of petroleum or oilstock processing can be used as said liquid as well as liquids close to said ones in their physical/chemical properties. These liquids are also used to partially substitute the liquid circulating at the second stage of compression. All these measures decrease environmental pollution and enhance ecological reliability of the plant for producing vacuum in the vacuum oilstock distillation column.
  • a gas-gas ejector At the first stage of the claimed plant a gas-gas ejector is used, it is fed with a high-pressure gas (an ejecting gas) being steam produced in the steam generator from the water-containing condensate obtained in the additional separator during the separation of the vapour phase condensate to the water-containing and the hydrocarbon-containing condensates.
  • a high-pressure gas an ejecting gas
  • the water-containing condensate is a water condensate in a case of complete phase separation occurred in the additional separator, or it is a mixture of water condensate and a small amount of a hydrocarbon condensate in a case of incomplete phase separation.
  • vapour-gas medium pumped out of the column contains a significant amount of steam that requires a lot of energy for its compression.
  • Further water vapour produced in the steam generator from the water-containing condensate will be referred to as steam.
  • water-containing condensate circulates at the first stage of compression of the vacuum producing plant within the following contour:
  • a portion of steam (water vapour) from the steam generator can be fed to the gas-gas ejector as a high-pressure gas, and the other portion of steam (water vapour) can be fed again to the vacuum oilstock distillation column and/or to the oilstock heated in the furnace prior to supply it to the vacuum column.
  • Steam the steam generator supplies can be additionally heated in the furnace using the heat of hot gases. This enhances operation properties of the steam.
  • a portion of steam from the steam generator can be supplied to the vacuum oilstock distillation column via additional gas-gas ejector connected at the low-pressure inlet to the pipeline for discharging vapour-gas medium from the vacuum column.
  • This allows amount of steam fed from the steam generator to the vacuum column and vapour-gas medium flow to the gas-gas ejector to be reduced. The latter circumstance leads to reducing steam flow from the steam generator to the gas-gas ejector. All the above decreases condenser heat load, reduces its size and energy consumption.
  • the condenser can comprise phase separator wherein a biphasic mixture supplied thereto from vapour condenser (condensation zone) separates into a vapour phase condensate and a gas mixture, wherein the gas mixture outlet of the phase separator is connected to its inlet to the liquid-gas jet device, and the vapour phase condensate outlet of the phase separator is connected to its inlet to the additional separator.
  • phase separator allows more complete separation of a gas mixture which has not been condensed in the condenser from the vapour phase condensate formed during its cooling.
  • Figure 1 represents a scheme of a plant for producing vacuum in a vacuum oilstock distillation column.
  • Figure 1 represents a scheme of a plant for producing vacuum in vacuum oilstock distillation column 1 with pipeline 2 for supplying oilstock connected thereto, pipeline 3 for supplying steam, pipeline 4 for evacuating distillate from vacuum column 1, pipeline 5 for evacuating distillation residue, pipeline 6 for discharging vapour-gas medium.
  • the plant for producing vacuum comprises gas-gas ejector 7, condenser 8, liquid-gas jet device 9, separator 10, pump 11 and additional pump 12.
  • Gas-gas ejector 7 is connected to pipeline 6 for discharging vapour-gas medium from vacuum column 1 at low-pressure gas inlet 13, at vapour-gas mixture outlet 14 it is connected to inlet 15 of the condenser 8 having vapour phase condensate outlet 16 and gas mixture outlet 17 connected to its inlet 18 to gas-liquid jet device 9.
  • Gas-liquid jet device 9 is connected to the outlet of pump 11 at liquid inlet 19, at gas-liquid mixture outlet 20 it is connected to separator 10 having compressed gas outlet 21 and liquid outlet 22 connected to the inlet of pump 11.
  • the plant is provided with steam generator 23, additional separator 24, pipeline 25 for supplying petroleum or oilstock distillate, pipeline 26 for evacuating petroleum or oilstock distillate from the plant.
  • Additional separator 24 is connected to vapour phase condensate outlet 16 of condenser 8 at inlet 27, at hydrocarbon-containing condensate outlet 28 it is connected to pipeline 29 for its evacuation from the plant, at water-containing condensate outlet 30 it is connected to the inlet of additional pump 12, the outlet of additional pump 12 is connected to water-containing condensate inlet 31 of steam generator 23, steam outlet 32 of steam generator 23 is connected to high-pressure gas inlet 33 of gas-gas ejector 7.
  • Steam generator 23 at heating agent inlet 34 is connected to pipeline 25 for supplying petroleum or oilstock distillate, at heating agent outlet 35 it is connected to pipeline 26 for evacuating petroleum or oilstock distillate from the plant.
  • Steam generator 23 can have non-evaporated condensate outlet 36 connected to additional separator 24.
  • Heat exchanger 37 can be installed between non-evaporated condensate outlet 36 of the steam generator and additional separator 24 inlet.
  • Steam outlet 32 of steam generator 23 can additionally be connected to pipeline 3 for supplying steam to vacuum column 1 and/or pipeline 2 for supplying oilstock thereto.
  • Additional gas-gas ejector 38 connected at low-pressure gas inlet 39 to pipeline 6 for discharging vapour-gas medium from vacuum column 1 can be installed at pipeline 3 for supplying steam into vacuum column 1.
  • Condenser 8 can comprise steam condensation device 40 connected to phase separator 41 separating a biphasic mixture supplied thereto into a condensate and a gas mixture.
  • Pipeline 25 for supplying distillate to steam generator 23 can be connected to pipeline 4 for evacuating distillate from vacuum column 1 or to pipeline 42 for evacuating distillate from atmospheric of high pressure petroleum distillation column 43.
  • Furnace 44 for heating oilstock can be installed at pipeline 2 for supplying oilstock to the vacuum column.
  • Steam outlet 32 of steam generator 23 can be connected to inlet 33 of gas-gas ejector 7 and/or to pipeline 3 for supplying steam to vacuum column 1 via steam heating pipes (that are not depicted on Fig. 1 ) of furnace 44.
  • Cooling heat exchanger 45 can be installed between liquid outlet 22 of separator 10 and liquid inlet 19 of liquid-gas jet device 9.
  • An excess of water-containing condensate can be evacuated from the plant via pipeline 46, in a case there is not enough water-containing condensate water or water condensate can be supplied via pipeline 47.
  • Steam generator 23 can have different constructive design and can comprise a set of elements e.g. economizer 48, evaporator 49, steam heater 50, non-vaporized condensate separator 51 and other interconnected elements. But any construction of steam generator 23 comprising different number of elements connected to each other is intended for attaining the same purpose namely to produce steam from the water-containing condensate by supplying a heat of a hot distillate fed via pipeline 25 and passing through the steam generator.
  • economizer 48 e.g. economizer 48, evaporator 49, steam heater 50, non-vaporized condensate separator 51 and other interconnected elements.
  • Oilstock black oil
  • vacuum column 1 having a top pressure 0.6 ... 6.0 kPa for distillation.
  • Steam is supplied to vacuum oilstock distillation column 1 via pipeline 3.
  • Steam can be supplied to vacuum oilstock distillation column 1 together with oilstock via pipeline 2.
  • a distillate e.g. vacuum gas oil
  • a vapour-gas medium which is a mixture of gas, light hydrocarbon vapours and water vapour is evacuated from the top of vacuum column 1 via pipeline 6.
  • Vapour-gas medium from vacuum column 1 is supplied to gas-gas ejector 7 wherein steam (water vapour) from steam generator 23 is supplied via inlet 33 as a high-pressure gas. Steam pumps out and compresses the vapour-gas medium which is fed to inlet 13 of gas-gas ejector 7 as a low-pressure gas. Compression occurs due to a transfer of kinetic energy from the high-pressure gas (water vapour) to the low-pressure gas in the course of their mixing in gas-gas ejector 7. As a result a pressure of a vapour-gas mixture at the outlet of ejector 7 becomes greater than a pressure of a vapour-gas mixture at its inlet.
  • vapour-gas mixture from ejector 7 is supplied to inlet 15 of condenser 8 wherein it is cooled due to a heat transfer through its wall to a cooling agent e.g. water having initial temperature of from 5°C to 35°C.
  • a vapour phase condensate forms, which is a mixture of water vapour condensate and a condensate of hydrocarbon vapours present in the vapour-gas mixture.
  • a separation of vapour phase condensate from a gas mixture (a non-condensed portion of the vapour-gas mixture) is carried out in condenser 8.
  • Condenser 8 can consist of phase separator 41 and vapour condensation device 40 connected thereto for better separating the vapour phase condensate from the gas mixture.
  • vapour phase condensate is supplied to additional separator 24 from condenser 8 via outlet 16.
  • the vapour phase condensate is separated in additional separator 24 to a water-containing condensate (water condensate in a case of 100% phase separation) and hydrocarbon-containing condensate (hydrocarbon condensate in a case of 100% phase separation).
  • the hydrocarbon-containing condensate is evacuated from additional separator 24 via outlet 28 to pipeline 29 for its discharging from the plant, and water-containing condensate is pumped out from outlet 30 using additional pump 12 to feed it to inlet 31 of steam generator 23.
  • An excess of the water-containing condensate is evacuated from the plant via pipeline 46.
  • Heat of a heating agent is supplied to the water-containing condensate in steam generator 23 to produce steam (water vapour) which is supplied to gas-gas ejector 7 as a high-pressure (ejecting) gas.
  • a heating agent is fed to inlet 34 of steam generator 23 via pipeline 25 for supplying petroleum or oilstock distillate.
  • pipeline 25 can be connected to pipeline 42 for evacuating distillate from petroleum distillation column 43 or to pipeline 4 for evacuating distillate from vacuum oilstock distillation column 1.
  • Spent heating agent from steam generator 23 is discharged from outlet 35 into pipeline 26 for evacuating petroleum or oilstock distillate from the plant.
  • non-vaporized portion thereof is separated from steam e.g. in separator 51 and evacuated from steam generator 23 via outlet 36 into additional separator 24.
  • heat exchanger 37 for cooling the non-vaporized condensate can be installed at the pipeline between the condensate outlet 36 of steam generator 23 and the condensate inlet of additional separator 24.
  • a gas mixture from the first compression stage namely from condenser 8 having a pressure of 3.5 ... 9.0 kPa via outlet 17 is fed to inlet 18 of liquid-gas jet device 9 of the second compression stage.
  • the gas mixture is a mixture of a gas and light hydrocarbon fractions and water vapour not condensed in condenser 8.
  • liquid-gas jet device 9 the gas mixture is compressed by virtue of energy of the liquid fed therein via inlet 19 using pump 11.
  • cooling heat exchanger 45 of the second stage of compression of the plant for producing vacuum a heat of the liquid arising both from mechanic energy dissipation in the liquid circulation contour and a condensation of vapours and cooling the gas in liquid-gas jet device 9 is transferred into the environment. This ensures temperature stabilization of the liquid in its circulation contour.
  • the gas-liquid mixture is separated into a compressed gas and a liquid in separator 10.
  • the compressed gas is supplied to a fueling system of the enterprise via outlet 21, and the liquid is supplied to the inlet of pump 11, thus closing liquid circulation contour. In this contour the liquid flows from pump 11 to liquid-gas jet device 9 and further to separator 10, leaving the latter it returns to the inlet of pump 11.
  • An excess of the liquid formed due to condensed vapours of hydrocarbon fractions and water vapour fed to liquid-gas jet device 9 with the gas mixture, and optionally supplied from an external source of a fresh liquid to the inlet of pump 11 or into separator 10 via pipelines 52 is evacuated from separator 10 via pipeline 53.
  • a hydrocarbon-containing liquid close in physical/chemical properties to the condensate of hydrocarbon fractions fed to liquid-gas jet device 9 with the gas mixture e.g. diesel fraction.
  • water vapour condensate is separated from the liquid in separator 10 and evacuated from separator 10 together with the excess of the liquid via pipeline 53 or a separate pipeline 54.
  • water is possible to use water as a fresh liquid.
  • a condensate of hydrocarbon fractions is separated in separator 10 and evacuated from separator 10 together with the excess of the liquid (as a mixture with water) via pipeline 53 or a separate pipeline 54.
  • a portion of water vapour from steam generator 23 can be fed to gas-gas ejector 7, and the other portion of the vapour can be fed to pipeline 3 for supplying steam to vacuum column 1 and/or to pipeline 2 for supplying oilstock.
  • Additional gas-gas ejector 38 connected at low-pressure gas inlet 39 to pipeline 6 for discharging vapour-gas medium from the vacuum column can be installed at pipeline 3 for supplying steam from steam generator 23 to vacuum column 1.
  • steam fed to ejector 38 as a high-pressure gas will pump out a portion of vapour-gas medium containing water vapour from pipeline 6 and feed it back to vacuum column 1. This will allow both an amount of steam supplied from steam generator 23 to vacuum column 1 and vapour-gas medium fed to inlet 13 of gas-gas-ejector 7 to be reduced.
  • Proposed method and plant as subject matters of invention could be used for producing vacuum a vacuum distillation column for distilling another raw material that differs from the oilstock e.g. in petrochemical or chemical industry.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
EP08865376.1A 2007-12-20 2008-11-06 Method and device for producing vacuum in a petroleum distillation column Not-in-force EP2239027B1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
RU2007147055/15A RU2354430C1 (ru) 2007-12-20 2007-12-20 Способ создания вакуума в вакуумной колонне перегонки нефтяного сырья и установка для осуществления способа
PCT/RU2008/000692 WO2009082263A1 (en) 2007-12-20 2008-11-06 Method and device for producing vacuum in a petroleum distillation column

Publications (3)

Publication Number Publication Date
EP2239027A1 EP2239027A1 (en) 2010-10-13
EP2239027A4 EP2239027A4 (en) 2012-09-05
EP2239027B1 true EP2239027B1 (en) 2015-02-18

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EP08865376.1A Not-in-force EP2239027B1 (en) 2007-12-20 2008-11-06 Method and device for producing vacuum in a petroleum distillation column

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US (1) US8337672B2 (es)
EP (1) EP2239027B1 (es)
BR (1) BRPI0821222A2 (es)
ES (1) ES2536408T3 (es)
RU (1) RU2354430C1 (es)
WO (1) WO2009082263A1 (es)

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8567299B2 (en) * 2010-11-22 2013-10-29 Vanair Manufacturing, Inc. Pressurized fluid delivery system and method of use
EA017594B1 (ru) * 2012-04-16 2013-01-30 Гумер Гарифович Теляшев Способ создания вакуума в аппаратах для перегонки нефтепродуктов и вакуумсоздающая система
CN103820216A (zh) * 2012-11-16 2014-05-28 北京中天金谷粮油工程技术有限公司 一种浸出溶剂回收节能器
RU2544237C1 (ru) * 2013-08-13 2015-03-20 Светлана Изаковна Сельская Способ переработки углеводородного сырья
RU2553825C1 (ru) * 2014-06-17 2015-06-20 Государственное унитарное предприятие "Институт нефтехимпереработки Республики Башкортостан" (ГУП "ИНХП РБ") Способ перегонки мазута
US20160115392A1 (en) * 2014-10-24 2016-04-28 Uop Llc Process for increasing a diesel recovery from a fractionation column
RU2678329C2 (ru) * 2017-05-05 2019-01-28 Рустем Руждиевич Везиров Способ конденсации парогазовой смеси из промышленных аппаратов вакуумной перегонки нефтепродуктов.
CN108579115A (zh) * 2018-05-04 2018-09-28 绵阳科大久创科技有限公司 一种负压蒸发精馏组合分离装置

Family Cites Families (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3796640A (en) * 1973-02-20 1974-03-12 Sybron Corp Vapor compression distillation
US4175034A (en) * 1978-10-10 1979-11-20 Uop Inc. Closed-loop vacuum fractionation process
US4690733A (en) * 1985-03-20 1987-09-01 Union Carbide Corporation Process for the separation of hydrocarbons from a mixed feedstock
JP3411280B2 (ja) * 1992-09-21 2003-05-26 協和醗酵工業株式会社 血小板減少症治療剤
RU2086603C1 (ru) 1993-04-23 1997-08-10 Виталий Галеевич Ахметов Способ разделения на фракции нефтяных масел, мазута или гудрона, способы создания вакуума и конденсации паров дистиллята с верха вакуумной колонны и устройство для осуществления способов
RU2091117C1 (ru) * 1995-12-22 1997-09-27 Валерий Григорьевич Цегельский Установка для перегонки жидкого продукта
US5762763A (en) * 1996-09-11 1998-06-09 Flair Corporation Method and apparatus for separating water from compressed air system condensate
DE59610308D1 (de) * 1996-11-19 2003-05-08 Sulzer Chemtech Ag Winterthur Destillationsanlage mit Wärmepumpe
RU2102103C1 (ru) 1997-01-22 1998-01-20 Пильч Леонид Моисеевич Способ вакуумной перегонки жидкого продукта и установка для его осуществления
RU2108365C1 (ru) * 1997-02-14 1998-04-10 Сергей Анатольевич Попов Установка для перегонки жидкого продукта (варианты)
RU2114893C1 (ru) * 1997-09-04 1998-07-10 Сергей Анатольевич Попов Способ перегонки многокомпонентной смеси и установка для его осуществления
RU2158623C1 (ru) * 1999-06-16 2000-11-10 Цегельский Валерий Григорьевич Способ сжатия и подачи под давлением углеводородосодержащих газообразных сред (варианты)
ES2305341T3 (es) * 2001-12-29 2008-11-01 Energy Saving Technologies Financial Industrial Group Llc Metodo para procesar mezclas liquidas multicomponentes y dispositivo para realizar dicho metodo.
US7267747B2 (en) * 2003-03-26 2007-09-11 Chevron U.S.A. Inc. Plant and method for vacuum distillation of hydrocarbon liquids
US7328591B2 (en) * 2003-09-19 2008-02-12 The Texas A&M University System Jet ejector system and method
US20060254280A1 (en) * 2005-05-12 2006-11-16 Siemens Westinghouse Power Corporation Combined cycle power plant using compressor air extraction
RU2304016C1 (ru) * 2005-12-29 2007-08-10 Валерий Григорьевич Цегельский Способ очистки от углеводородов парогазовой среды, образующейся при хранении нефти или бензина или при наполнении емкости нефтью или бензином, и установка для его осуществления (варианты)
RU2310678C1 (ru) * 2006-03-07 2007-11-20 Валерий Григорьевич Цегельский Способ вакуумной перегонки сырья, преимущественно нефтяного сырья, и установка для осуществления способа (варианты)

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WO2009082263A1 (en) 2009-07-02
BRPI0821222A2 (pt) 2015-06-16
RU2354430C1 (ru) 2009-05-10
US8337672B2 (en) 2012-12-25
EP2239027A1 (en) 2010-10-13
ES2536408T3 (es) 2015-05-25
EP2239027A4 (en) 2012-09-05

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